Method of purifying thiocyanate solutions



LEM.

METHOD or rumrunvo THIOCYANATEI SOLUTIONS Victor C. Serreze, Jr., Cos Cob, ConnQ a'ssi gnorto American Cyanamid Company, New York, -N. Y., a corpora tionofMaine w No Drawing. Filed A nea, 1958 ,Ser. No. 130,247

'5Claims. or. 23-15 and, more particularly, to the purification of thiocyanate solutions, especially such solutions which are tobe used or re-used as the solvent component of a spinning solution, e.g., one comprised of a polymer of acrylonitrile.

In the production of staple fibers, continuous filaments (-monoand multifilaments), rods, tubes, films, ribbons,

sheets, and other shaped articles from a solution of a polymer of acrylonitrile dissolved in a concentrated aqueous solution of sodium thiocyanate or other watersoluble thiocyanate (with or without one or more other additives such as a lower monoh-ydric alcohol), dilute solutions of the thiocyanate are obtained. (Such processes 3 are described in, for example, Cresswell US. Patents 2,558,730, -1, -2, -4, and -5, all dated July 3, 1951; Cresswell and Wizon US. Patent No. 2,558,733 "and Pollard US. Patent No. 2,558,781, each dated July: 3',

1951; and British Patents 714,530, 715,915, 729,472, a'nd 732,135.) It is important to the e'conomicsof the process that such dilute solutions be concentrated 1 and the con centrated thiocyanate solution then reused'in the; process Otherwise the manufacturing costs maybe prohibitive from a competitive standpoint.

In making polyacrylonitrile fibers from solutions-of the kind described in the preceding paragraph, and specifically from a polymer of acrylonitrile dissolved-in a concentrated aqueous solution of sodium thiocyanate, it

was discovered that, after spinning forflvaryingperiods of time, the spinnerette openings became. obstructed, jcaus ing unsatisfactory spinning operations andthe production of fiber of inferior quality, :and eventually thetshut down of the spinning device for replacement of'the spinnerette with one having unobstructed openings. The contaminated spinnerette then had to be cleaned. This was costly and time-consuming. Analytical. studies revealed that the material that was obstructing the'spinn'erette holes comprised mainly sodium sulfate, which also was found tobe present in the spinning solution or'fdope and also, 1 in the thiocyanate solution in .whichthe. acrylonitrilepolymer was dissolved tomake: thei 'dope. (The sodium sulfate may result, for examplefrom'sulfoxycompounds used as the reducing agent of ya redox-catalyst system employed in the polymerization opera ion.) Other impurities found in recovered sodium-thiocyanate solution include CO Cl-,.CN N035, Fe'+ Aland Cu+ "l v The presence of sodium sulfate in the dilute '(eLg.', -2 to"20% by weighty sodium thiocyanate solution is also objectionable when concentrating the solution for re-use'" in the process, since it causes scalebuild-up in evaporatoisduring evaporation of the solution. h

7 One solution to the above-described problem, which is" solely'a particular kind o'f'a chemical treatment, is disclosed and claimed in the cop'ending'application'of Victor soluble barium compound can be used.

CJSerreze, Jr., and Witold R. Kocay, Serial No.1689,7,85,

filed October 14,1957. The present invention isa differ ent solution to thesame problem. t

*It is a primary object of the-presentinvention to pro wide, a imp e and. .iuezasns metgsd at. rgmq ins 2,977,188 Patented Mar. 28,1961

purities comprising mainly sodium sulfate, as well as other impurities such as those mentioned above, from an aqueous'solution of sodium thiocyanate containing the ing water under heat '(e.g., at a temperature of from-' 50 C. to 130 C., and preferably under sub-atmospheric pressure, i.e., under vacuum) from a 2% to 20%, by Weight, aqueous solution of sodium thiocyanate containing sodium sulfate and other impurities. The evaporation is caused to take place, preferably continuously, until the solution contains between about 56% and about 62% by weight of NaSCN. During evaporation of the water, that part of the total amount of sodium sulfate which is in excess of the solubility of Na SO in the concentrated thiocyanate solution is precipitated therefrom. The resulting concentrated solution of sodium thiocyanate is then cooled to a temperature below 38 C. but above the freezing point of the concentrated thiocyanate solution. This causes an additional amount of sodium sulfate to separate, moreparticularly crystallize, from the cooled solution, after which it'is removed from the solution, e.g., by filtration, centrifuging, decanting, etc. The evaporation step briefly described above can be effected in commercially available evaporators, using suitable materials of construction that will resist the corrosive influences of aqueous sodium thiocyanate solutions. The evaporation may be effected in stages, during which part of;th e water is removedat atmospheric pressure and the remainder-at reduced pressure, e.g., at a-pressure in the final stage that may be as low,if desired, as 10 mm. Hg pressure (or even lower) but which generally isnot lower than about 150 mm. Hg pressure, at which pressure the final temperature will generally range between about c. and 0.;

A modification ofthe present invention has as its primary object a preliminary chemical treatment of the starting 2% to 20%, by weight, aqueous solution of sodium thiocyanate whereby precipitation in the evaporator. (i.e.,-on the evaporator surfaces) of that part of the total amount. of sodium sulfate which is in excess of the solubility. of, Na SO in the concentrated thiocyanate solution is obviated or minimized; -At least part of this precipitated sodium sulfate forms a scale on the evaporator surfaces. As a result it is necessary, in'order to maintain the. efliciency of the evaporator, to discontinue operation of the evaporator and remove the aforementioned scale. This is costly and time-consuming.

Thepreliminary chemical treatment mentioned in the preceding paragraph comprises admixing with the starting 2% to 20%, by weight, aqueous solution of sodium thiocyanate containing sodium sulfate and-other impurities .anamount of a water-soluble barium compound which is substantially less than the chemical equivalent amount required for converting all -of:the said sodium sulfate to barium sulfate, but which is suflicient to prevent the precipitation of sodium sulfate during subsequent concentration under heat of the said thiocyanate solution. Thereafter the precipitate (precipitated material) comprising barium sulfate is separated from the resulting thiocyanate solution, e.g., by filtration, centrifuging, decanting, etc. To the best of my knowledge and belief, any water- Illustrative examples ofsuch compounds are barium hydroxide [Ba(OH) 2 8H 0] barium nitrate, barium acetate, barium thiocyanate, barim tbensa tet me. arium, buty ae. ba iu chlorate, barium formate, barium chloride, etc. It is not necessary that the chosen water-soluble barium compound be one that has been preformed before addition to the aqueous thiocyanate solution. Instead. one/can use reagents that will react with each other to form a water-soluble barium compound in situ. Examples of such reagents are barium hydroxide and ammonium thiocyanate which can be added to the aqueous thiocyanate solution and will react with each other to form barium thiocyanate in situ.

The method of this invention is especially applicable in the treatment of dilute solutions of sodium thiocyanate, that is, solutions containing from about 2% to about 20%, more particularly from about 3% to about by weight of NaSCN, and whichalso contain sodium sulfate as an impurity. However, aqueous sodium thiocyanate solutions containing above by weight of NaSCN (e.g., up to about 55% by weight of NaSCN) and containing Na SO as an impurity also can be effectively treated in accordance with this invention.

it is important that one determine, as by known chemical or. other analytical techniques, the amount of sodium sulfate which is present in the sodium thiocyanate solution prior to adding the water-soluble barium compound thereto. As stated above, the amount of the latter should be substantially less than the chemical equivalent amount required for converting all of the sodium sulfate to barium sulfate, but which is sufficient to prevent the precipitation of sodium sulfate during subsequent concentration under heat of the said thiocyanate solution. Knowing the total amount of sodium sulfate in the starting thiocyanate solution and from a previously prepared graph showing the solubility of Na SO in aqueous. NaSCN over the range of concentrations and temperatures encountered in the concentration ofthe thiocyanate solution, one can calculate the amount of watersoluble barium compound that will remove enough sodium sulfate so that none (or no appreciable amount) of the latter will be precipitated on the evaporating surfaces of the evaporator.

The temperature of treating with the water-soluble barium compound isnot critical and may range, for example, from 10 to 30 C. or at higher temperatures up to the boiling temperature of the thiocyanate solution at'atmospheric pressure. i

At any stageof'the treatment of the sodium thiocyanat solution with thewater-soluble barium compound, orat the end of the treatment with thesaid compound, there'may be added to the thiocyanate solution a finely divided adsorbent, more particularly a decolorizing agent, e.g., finely divide d activated carbon, bone black, certain natural or activated bleaching clays, etc., and/or a filter aid, e.g., finely divided diatornaceous earth. The adsorbent, e.g., a decolorizing agent, improves the color of the thiocyanate solution and adsorbs other impurities such,

for example, as hydroxides of iron and copper that may be present. Removal of such impurities decreases color formation in aqueoussodium thiocyanate solutions as well as in the ,final polyacrylonitrile fiber made from ,the spinning solution. i

The amount of adsorbent and/or filter aid employed is not critical and may be varied as desired or as conditions may require, e.g., from 0.05% to 1 or 2% by weight of the thiocyanate solution.

In order that those skilled in the art may better understand how the present invention can be carried into cffect the following examples are given by way of. illus;

tration and not by way of limitation. All parts and-per centages are by weight unless otherwise stated.v In all examples the content of sodium sulfate in the thiocyanate solution was determined prior to the processing operations described in the individual example.

Example 1 A dilute aqueous solution of sodium thiocyanate-conn nies taining about 10% NaSCN and 0.37 lb. of Na SO per lbs. of actual NaSCN is evaporated to a concentration of about 61% NaSCN under a reduced pressure of 200 mm. Hg pressure in the final stages of the concentration, and at a maximum liquor temperature in the final stages of the concentration of about 120 C. At thistemperature only 0.29 lb. of Na SO per-100 lbs. of actual NaSCN is held in solution. This means that 0.08 lb. of Na SO per 100 lbs. of actual NaSCN, or 21% of the total sulfate initially present, precipitates out in the evaporator.

The resulting concentrated solution of sodium thiocyanate is run into a, crystallizer and cooled to 35 C. About 0.22 lb. of Na SO per 100 lbs. of actual NaSCN crystallizes out of-solution, and is removed by filtration. The amount removed in this way is 60% of the Na SO present in the initial solution, and a total of 81% of the Na SO initially present isremoved by the combined steps. The purified NaSCN solution can be diluted with waterto any desired strength required for use as a solvent-for a polymer of acrylonitrile in making a spinning solution or for any other purpose.

' Example 2 A polyacrylonitrile dope (spinning) solution prepared by dissolving about 10% of a polymer of acrylonitrile in about 48%. sodium thiocyanate nearly saturated with sodium sulfate. is extruded through a spinnerette into a coagulatingbath comprised of a 10% aqueous solution of'NaSCN' and maintained at a temperature of about 1 0; Equilibrium of the coagulating solution is attained. with the, result that the. sodium sulfate level reaches alevel of-0.60 lb. ofNa SO per 100 lbs. of actual- NaSCN. Recovery of sodium thiocyanate is achievedby evaporation-of the water under vacuumin an evaporator at approximately 200- mm. Hg pressure. Evaporation. is-carriedout to a final concentration of 56.5%, aqueous sodium thiocyanate. The final liquor temperature in the evaporator at this concentration is approximately C. At 110 C. only 0.32 lb. sodium sulfatefper 100 lbs. of sodium thiocyanate remains in solution with the result that 0.28 lb. of sodium sulfate per l00..lbs. of: actual sodium thiocyanate precipitates out in the.evaporator. This-corresponds to about-46.7% removal of the original total sodium sulfate in the starting thiocyanate solution.

The concentrated thiocyanate solution or slurry is pumpedfromthe evaporator and fed to a crystallizer. Theslurry is cooled to 21 C. (3 C. above the freezing point of.56.5 aqueous sodium thiocyanate), whereupon an additional. amount of Na SO separates in crystalline form. t The resulting slurry is filtered The-mother liquor now contains 0.11 lb, of sodium sulfate per 100 lbs. of actual sodium thiocyanate. Thus.0.21 lb. of sodium sulfate per 100 lbs. of sodium thiocyanate has been removeddnthecrystallizer or 35% of the total original sodium sulfate. Total sodium sulfate removal in the two steps is, therefore, 81.7%.

' Example 3 A polyacrylonitrile dope or spinning solution prepared by diss'olving-about 10% of a polymer of acrylonitrile in about. 46% aqueous sodium thiocyanate solution containing about,0.65 lb. of Na SO per 100 lbs. of actual NaSCN is; extruded through a spinnerette. into a coagulating bath comprised of a 7% aqueous solution of NaSCN and maintained at a temperature of about 1 C. Equilibriumof :the. coagulating solution isattained with theresult that the lattercontains about 0.65 lb. of Na SO per 100. lbs. or actual NaSCN.

2 The dilutethiocyanate solution from thecoagulating bath is evaporated to 59%; NaSCN concentration in an evaporator under increasingly higher vacua which, in its final stages, corresponds to 200 Hg pressure. At this point the liquor temperature corresponds to C.-and

After filtration of the 'hot liquor from the: evaporator.

the .elfiuent is allowed to cool in a crystallizer, with seeding with a few crystals of sodium sulfate, to a temperature of 25 C. (3 C. above the freezingi'point of 59% sodium thiocyanate), and the slurry containing the Na SO that hascrystallized out is filtered. 'The filtrate has a sulfate content of 0.07 lb. of sodium" sulfate; perj 1 lbs. of actual sodium thiocyanate. I Removal in this step amounts to 35.4% of the te n br'i inlis diun sulfate; 'iTotal removal of Na SO in the combined steps amounts to about 89% of the original amount present'in the thiocyanate solution. v

Example 4 v A polyacrylonitrile spinning solution prepared by dissolving about 10% of'a polymer of acrylonitrile in about 50% aqueous sodium thiocyanate solution containing about 0.52 lb. of Na SO per 100 lbs. of actual NaSCN is extruded through a spinnerette into a coagulating bath comprised of a 15% aqueous solution of NaSCN and maintained at a temperature of about 1 C. Equilibrium of-the coagulating solution is attained with the result that the latter contains about 0.52 lb. of Na SO per 100 lbs. of actual NaSCN.

The dilute thiocyanate solution from the coagulating bath is evaporated to 62% NaSCN concentrationin essentially the same manner described under Example 3, the final liquor temperature being 120 C. At this tern; perature 0.28 lb. of Na SO4 per 100 lbs. of actual NaSCN remains in solution, and 0.24 lb. of Na SO per 100 lbs. of actual NaSCN is precipitated out in the evaporator. This correpsonds to the removal of about 46% of the total original Na SO content.

After filtration of the hot liquor, the filtrate is cooled in a crystallizer to a temperature not lower than 35 C. The amount of Na SO which crystallizes,out in this stage is 0.23 lb. per 100 lbs. of actual NaSCN, or about 44% of the total content of Na SO in the original NaSCN solution. Total removal of Na SO in the combined steps amounts to about 90% of the original amount present in the thiocyanate solution.

Example 5 ",-An.8%' aqueousNaSCN solution having an equilibrium Na sogcontent .ofm0.37 lb./ 100 lbs. actual NaSCN is treated with-0.0.0063 lb. moleuof Ba(NO Ian d with ammoniumhydtoxide. to bri s hepH t & A ivate carbon and diatomaceous earth (filter aid) are added, and the resulting slurry is agitated for one hour, and then filtered. The Na SO content of the NaSCN solution is now 0.28 lb./100 lbs. actual NaSCN, which corresponds to the removal of 24.0% of the original Na SO content. Evaporation of the dilute NaSCN solution is carried out in an evaporator as in the previous examples. In this case the vacuum in the final stage corresponds to 200 mm. Hg pressure, and evaporation is continued to a final concentration of 59% NaSCN. With the liquor temperature at 115 C. in the final stage, 0.30 lb. Na SO /100 lbs. actual NaSCN remains in solution.

The concentrated NaSCN solution is slowly cooled in a holding tank with a few crystals of Na SO added as seed. Cooling to 28 C. reduces the Na SO solubility to 0.08 lb. Na SO /100 lbs. actual NaSC-N. The crystallized Na SO is removed by filtration. Removal by crystallization amounts to 54%. Total removal by both steps amounts to 78%.

Example 6 A 12% aqueous NaSCN solution containing at equilibrium 0.35 lb. Na SO /100 lbs. actual NaSCN is treated with 0.00056 1b. m l of Ba(SCN) and with ammo: ni-um hydroxide to adjust the pH to 8:" Activated carbon and diatomaceous earth are added and the'resulting slurry is agitated for 1.5 hours and then filtered. The residual NA SO in the filtrate is 0.271 lb./100 lbs. actual NaSCN. This corresponds to the removal of22.5 of the original Na SO and a sulfate removal efliciency 'of'the chemical treatmentof98%. I

Evaporation to 62% NaSCN'is carried out as in prior examples at 200 mm. 'Hg' pressure in'the final stagetanld a final liquor temperature of 122" C.' At 122 C.', Na SO' is solublein the hot, concentrated thiocyanate solution to the extent of 0.285 lb./ lbs; actual NaSCN. Slow cooling of the hot concentratedliquoris conducted in a hold tank" with a few crystals'of Na SO added as seed. At a final temperature of 37 C., the liquor 'holds 0.065 lb. Na SO /100 lbs. actual NaSCN. The slurry is filtered to remove the crystalline Na SO that separates, and removal of sulfate by crystallization amount to 59% of the original. Total removal of Na SO in the combined steps is 81.5% of the total original amount present in the dilute thiocyanate solution. .1

Example 7 A polyacrylonitrile spinning solution prepared by dis-, solving a polymer of acrylonitrile in, a 48%} aqueous NaSCN solution and which contains 0.35 lb. 'Na SO 100 lbs. actual NaSCN is extruded into ;a coagulating bath comprised of a 10% aqueous NaSCN solution. Equilibrium is obtained in the coagulating bath in which the Na SO content is also 0.35 lb./100 lbs. actual NaSCN;

To the dilute NaSCN solution from the coagulating bath is added 0.00049 lb. mole of Ba(COCH and NH OH to bring the solution to a pH of 8. .The solution is agitated for one hour while admixed with activated carbon and diatomaceousearth which have been added thereto, and is then filtered. The filtrate contains 0.285 lb. Na SO /1O0 lbs. actual NaSCN, which corresponds to an efficiency of 94% for sulfate removal by barium acetate treatment, or a removal of about 18.6% of the original. total Na SO content of the NaSCN solution. 1 The solution is evaporated, as in priorexamples, to 61% NaSCN concentration at 200 mm. Hg pressure. vAt the final liquor temperature of C., in the evaporator, 0.29 lb. Na SO /100 lbs. actual NaSCN is held in solution. The evaporator efiluent (61% NaSCN) is slowly cooled to 35 C. with seeding with a few crystals .of Na SO at 35 C. only 0.07 lb. Na SO /100lbs. actualNaSCN remains, in solution. Thus 0.215 1b. Na SQ /100 lbs. actual NaSCN crystallizesout andgisremov ed by filtra tion. Removal. of Na SO .in this second step amounts to; about 61.4% of I the total- .original I Na' SO present; in the dilute NaSCN solution. The total removal of sodium sulfate in both steps is 80.0% of the original Na SO content of the starting thiocyanate solution.

Example 8 A dilute NaSCN solution from a coagulating bath ob tained as described in Example 7 and containing 0.35 lb. Na SO 100 lbs. actual NaSCN is used in'this example. To this solution is added 0.00049 lb. mole of Ba(OH) The pH of the resulting solution is 9. Activated carbon and diatomaceous earth are added'to this solution, and the mixture is agitated for one hour and then filtered. The filtrate contains 0.270 lb. Na SO 100 lbs. NaSCN. This represents the removal of about 22.8% of the original N a SO content of the NaSCN solution.

The solution is then evaporated, as in prior examples, to 62% NaSCN concentration at 200 mm. Hg pressure and a final liquor temperature of 122 C. in the evaporator. At this temperature Na SO is soluble to the extent of 0.285 lb./100 lbs. actual NaSCN. The hot liquor is slowly cooled to 37 C. in a crystallizer. At 37 C. the concentrated NaSCN solution holds 0.065 lb. Na SO /100 lbs. actual NaSCN. The remaining portion of Na SO 7 or.,0.2OSj lb. Na SO /1O0 lbs. actual NaSCN crystallizes utQan'd isremovedby filtration. This amountrepresents the remoy'alof ,al io-ut-58.6% of the. total Na SO present in the dilute NaSCN solution. The amount of Na SO removed by the combined steps represents about 81.4% of theoriginal Na SO content of thestarting thiocyanate solution.

. E ample) A dilute NaSCNsolution containing 0.37 lb. Na SO 100lbs. actual NaSCN is treated with 0.00057 lb. mole of Ba(OH) and-40.001114: lb. moleof NH SCN. The mixture is agitatedforone-hour at-20 C. The initial pHof the mixtureis 8.5 and, after agitating for one hour, thepH is 7.5. (The highinitialpI-I'of 8.5 is due to the evolution of ammonia during the ammonium thiocyanatebarium hydroxide reaction. This pH is suflicient to precipitate dissolved iron as the insolublehydroxide so that any iron irnpurity'also can be removed in the subsequent-filtration step.) Activated carbon (decolorizing carbon) and diatomaceous earth are added and the resulting mixture is filtered as in Examples 5, 6 and 7. The filtrate contains 0.29 lb. Na SO 100 lbs. actual NaSCN, which represents the removal of about 21.6% of the original Na SO content of the NaSCN solution.

The solution is evaporated, "as in prior examples, to 61% NaSCN concentration at 200 mm. Hg pressure and a final liquor temperature of 120 C. in the evaporator. The hot liquoris then cooled to 35 C. in a crystallizer and seeded with a few crystalsof Na SO At this temperature the 61% NaSCN- solution holds 0.07 lb. Na SO 100 lbs. actual NaSCN. The remaining portion of:Na SO or- ;22 1b. Na S0 /100' lbs. actual NaSCN crystallizes out and is removed by filtration. This amount represents the removal of about 59.4% of the total Na SO present in the dilute NaSCN solution. The amount of Na sOs, removed by the combined steps represents about 81% of the original Na SO content of the starting th-iocyanate solution.

I claim:

1. A method of purifying an impure dilute aqueous sodium thiocyanate solution, formed in synthetic fiber spinning, to a degree of purity such that after concentration it can be used asthe' solvent component of a spinning solution that will not obstruct spinnerette openings by depositing ilmpuriti'es therein, which comprises evaporating-water ine." single heating step from an aqueous 2% to 20%, by weight,- sodium thiocyanate solution from said source'havi-ng a pH of at least 7.5 and-containing small amounts of sodium sulfate and color-forming metallie compounds as impurities until the solution contains between about 56% and about 62% by weight of NaSCN and that part of the sodium sulfate which is in excess o fthe solubility of Na SO in the solution after concentration has precipitated, transferring the resulting con centrated sodium thiocyanate solution in a precipitatefree condition to a cooling zone, cooling it in said' zone to a temperature below 38 C. but above the freezing point of; the concentrated.thiocyanate solution andgmain: taini ng it at said temperature until substantially all of the residualsodiurnsulfate hasseparated therefrom, the aforesaid color-forming metallic compounds being removed in insoluble form from the" sodium thiocyanate solution alqng with the sodium sulfate by reason of its alkaline condition.

2. A method as in claim 1 wherein the water is evaporated from the 2% to 20%, by weight, aqueous solution of sodiumthiocyanate under reduced pressure to a maximum temperature not exceeding about C.

3. The method of removing impurities from a 2% to 20%, by weight, aqueous solutionof sodium thiocyanate containing sodium sulfate and other impurities which comprises admixing with said solution an amount of a water-soluble barium compound which is substantially less than the chemical equivalent amount required for converting all of the said sodium sulfate to barium sulfate, but which is suflicient'to prevent the precipitation of sodium sulfate during subsequent concentration under heat of the said thiocyanate solution and bringing the said solution to a pH of at least 7.5 during said admixing; separating the precipitate comprising barium sulfate from the thusly treated thiocyanate solution; evaporating water from the barium sulfate-free thiocyanate solution, in a single heating step, until the solution contains between about 56% andabout 62% by weight of NaSCN; transferring the resulting concentrated solution of sodium thiocyanate to a cooling zone;cooling the said solution in said zone to a temperature below 38 C. but above the freezing point of the concentrated thiocyanate solution, whereby sodium sulfate separates from the cooled solution; andremoving the said sodium sulfate from the said solution.

4. A method asin claim 3 wherein the water-soluble barium compound is barium hydroxide.

5. A method as in claim 3 wherein the water-soluble barium compound is barium thiocyanate.

References Cited in the file of this patent UNITED STATES PATENTS 737,740 Jacobs Sept. 1, 1903 2,313,680 Smith Mar. 9, 1943 2,459,302 Aronson Jan. 18, 1949 2,575,238 Stenger Nov. 13, 1951 

1. A METHOD OF PURIFYING AN IMPURE DILUTE AQUEOUS SODIUM THIOCYANATE SOLUTION, FORMED IN SYNTHETIC FIBER SPINNING, TO A DEGREE OF PURITY SUCH THAT AFTER CONCENTRATION IT CAN BE USED AS THE SOLVENT COMPONENT OF A SPINNING SOLUTION THAT WILL NOT OBSTRUCT SPINNERETTE OPENINGS BY DEPOSITING IMPURITIES THEREIN, WHICH COMPRISES EVAPORATING WATER IN A SINGLE HEATING STEP FROM AN AQUEOUS 2% TO 20%, BY WEIGHT, SODIUM THIOCYANATE SOLUTION FROM SAID SOURCE HAVING A PH OF AT LEAST 7.5 AND CONTAINING SMALL AMOUNTS OF SODIUM SULFATE AND COLOR-FORMING METALLIC COMPOUNDS AS IMPURITIES UNTIL THE SOLUTION CONTAINS BETWEEN ABOUT 56% AND ABOUT 62% BY WEIGHT OF NASCN AND THAT PART OF THE SODIUM SULFATE WHICH IS IN EXCESS OF THE SOLUBILITY OF NA2SO4 IN THE SOLUTION AFTER CONCENTRATION HAS PRECIPITATED, TRANSFERRING THE RESULTING CONCENTRATED SODIUM THIOCYANATE SOLUTION IN A PRECIPITATEFREE CONDITION TO A COOLING ZONE, COOLING IT IN SAID ZONE TO A TEMPERATURE BELOW 38*C. BUT ABOVE THE FREEZING POINT OF THE CONCENTRATED THIOCYANATE SOLUTION AND MAINTAINING IT AT SAID TEMPERATURE UNTIL SUBSTANTIALLY ALL OF THE RESIDUAL SODIUM SULFATE HAS SEPARATED THEREFROM, THE AFORESAID COLOR-FORMING METALLIC COMPOUNDS BEING REMOVED IN INSOLUBLE FORM FROM THE SODIUM THIOCYANATE SOLUTION ALONG WITH THE SODIUM SULFATE BY REASON OF ITS ALKALINE CONDITION. 